CN101439256B - Film method for recycling CO in high-pressure exhaust from production of acetic acid by carbonylation - Google Patents
Film method for recycling CO in high-pressure exhaust from production of acetic acid by carbonylation Download PDFInfo
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- CN101439256B CN101439256B CN200810235144XA CN200810235144A CN101439256B CN 101439256 B CN101439256 B CN 101439256B CN 200810235144X A CN200810235144X A CN 200810235144XA CN 200810235144 A CN200810235144 A CN 200810235144A CN 101439256 B CN101439256 B CN 101439256B
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- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 title claims abstract description 123
- 238000000034 method Methods 0.000 title claims abstract description 46
- 230000006315 carbonylation Effects 0.000 title claims abstract description 17
- 238000005810 carbonylation reaction Methods 0.000 title claims abstract description 17
- 238000004519 manufacturing process Methods 0.000 title description 5
- 238000004064 recycling Methods 0.000 title description 3
- 239000007789 gas Substances 0.000 claims abstract description 124
- 239000012528 membrane Substances 0.000 claims abstract description 32
- 238000000926 separation method Methods 0.000 claims abstract description 15
- 239000001257 hydrogen Substances 0.000 claims abstract description 9
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 8
- 230000006835 compression Effects 0.000 claims abstract description 4
- 238000007906 compression Methods 0.000 claims abstract description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 claims description 22
- 238000005273 aeration Methods 0.000 claims description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 239000002253 acid Substances 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 8
- 239000000835 fiber Substances 0.000 claims description 4
- 239000004642 Polyimide Substances 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 229920001721 polyimide Polymers 0.000 claims description 3
- 230000001681 protective effect Effects 0.000 claims description 2
- 239000000047 product Substances 0.000 abstract description 20
- 238000011084 recovery Methods 0.000 abstract description 15
- 230000008569 process Effects 0.000 abstract description 10
- 239000000463 material Substances 0.000 abstract description 6
- 239000012467 final product Substances 0.000 abstract 1
- 238000005406 washing Methods 0.000 abstract 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 12
- 238000000746 purification Methods 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 239000003463 adsorbent Substances 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 5
- WFDIJRYMOXRFFG-UHFFFAOYSA-N Acetic anhydride Chemical compound CC(=O)OC(C)=O WFDIJRYMOXRFFG-UHFFFAOYSA-N 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- INQOMBQAUSQDDS-UHFFFAOYSA-N iodomethane Chemical compound IC INQOMBQAUSQDDS-UHFFFAOYSA-N 0.000 description 3
- 239000011265 semifinished product Substances 0.000 description 3
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000008595 infiltration Effects 0.000 description 2
- 238000001764 infiltration Methods 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 229920013683 Celanese Polymers 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- OKJPEAGHQZHRQV-UHFFFAOYSA-N Triiodomethane Natural products IC(I)I OKJPEAGHQZHRQV-UHFFFAOYSA-N 0.000 description 1
- 241000276425 Xiphophorus maculatus Species 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 125000002915 carbonyl group Chemical group [*:2]C([*:1])=O 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000000994 depressogenic effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 235000012489 doughnuts Nutrition 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- -1 handle tolerance Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000011070 membrane recovery Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 239000010948 rhodium Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a method for recovering CO from a high-pressure acetic acid tail gas produced by carbonylation through a membrane process and a device thereof. The tail gas is treated by three steps, that is, pretreatment, membrane separation and gas compression: the tail gas that passes a gas washing tower, a demister and a combined filter enters a Prisen membrane separator through a heater, the tail gas after the membrane separation enters a compressor, a product gas is recovered and reused, and hydrogen rich gas flows to a torch for burning. In the method, two Prisen membrane systems help control the amount of the feed gas entering a membrane, the product gas and the hydrogen rich gas to reach N2 material balance, ensure the CO recovery rate and achieve the purpose of the long and stable operation of a membrane separation device; and the content of the CO in the final product gas is not less than 91%.
Description
Technical field
The present invention relates to the technology of purification CO from the mixed tail gas of production of acetic acid discharging, particularly carbonylation is produced the recovery method of CO in the acetate high pressure exhaust gas.
Background technology
Since early 1970s Pu Like proposes with carbon monoxide and carbonylation of methanol in U.S. Pat 3769329, adopt rhodium, methyl iodide, methyl acetate, water etc. as this technology after the method for Catalyst Production acetate by the complete industrialization in the world, all producing with this method more than 75% of present acetic acid total amount in the world, this method has advantages such as methyl alcohol selectivity height, purification is simple, technological process is compact, production cost is low.Though this method is produced the contribution of the optimization Processes for Producing Acetic Acid of making aspects such as acetic acid reaction liquid, catalyst research nearly decades at carbonylation through large-scale production of acetic acid enterprises such as U.S.'s Celanese, BP, Japan big plug road chemical industry Co., Ltd., but a series of patent and document have all illustrated carbon monoxide of reaction and methyl alcohol and can not reach 100% conversion, and carbonylation process has water gas reaction, produced hydrogen and carbon dioxide, comprised in the discharge tail gas in unreacted carbon monoxide, the unstripped gas with H
2, N
2, CH
4The carbon dioxide and the H that bring with carbon dioxide, side reaction
2Deng.Have materials such as methyl acetate, acetate, aceticanhydride from the high pressure exhaust gas of reactor exhaust outlet discharging with the form of full steam, harmfulness to human body is bigger, also be rich in simultaneously a large amount of CO, but because CO separation and recovery technology, purification CO technology limitation from gaseous mixture particularly, the tail gas majority is all done emptying and is handled at present, and the energy had both been wasted in a large amount of CO emptying, increase the cost of production of acetic acid, polluted environment again.Therefore, seek technology that a kind of advantages of simplicity and high efficiency reclaims acetate acid tail gas and become the direction that acetic acid technical research person, the producer make joint efforts.
In China, the PU-1 adsorbent of Beijing University exploitation is the adsorbent of purification CO function admirable from mist at present, makes China's CO purification technique reach advanced international standard.NHD (key component is a NHD) method: this method is a kind of novel C O purification technique by the exploitation of China southization institute, to H
2S, COS, CO
2Various acidity and non-acid gases all have stronger solvability, and can optionally absorb H
2S and COS.This method technological process is simple, reduced investment, and NHD solution reproducible utilization, and chemical stability, Heat stability is good are because the NHD solvent is to H
2, N
2, CH
4Do not have bigger dissolubility Deng gas, so can not be applied to the purification of CO in the acetate acid tail gas.
The pressure swing adsorption method mature technique is promoted rapidly and is used in the technical process of purification CO, because the economic worth of acetate acid tail gas, make people that both are combined, produce transformation absorption and reclaimed acetate acid tail gas technology: removed objectionable impurities such as iodomethane, methyl alcohol by pretreatment unit, enter the PSA-1 operation again, the weak absorbent components H in the unstripped gas
2, CO, N
2Flow out Deng upper end, obtain semi-finished product gas, send into PSA-2 purification CO, strong absorbent components CO from adsorption tower
2, H
2O is attracted on the adsorbent, and desorbs from adsorbent with step-down and flushing process, and adsorbent obtains regeneration, is used for next circulation.After semi-finished product gas entered the PSA-2 operation, CO belonged to the strongest absorbed component in semi-finished product gas, at first was attracted on the adsorbent, and all the other components flow out from the port of export of adsorption tower, as the regeneration purge gas of PSA-1.After adsorption process finished, a part of products C O that backflows is as the displacement gas of adsorbent bed, and was last to improve the purity of CO in the bed, put and find time to obtain CO more than 98% by contrary, and the rate of recovery reaches 70%-85%.
The subordinate of Suo Pu group acetic acid factory takes carbonyl process to produce acetic acid, handle by the method for burning at present, according to present environmental protection pressure, economic worth that high pressure exhaust gas is recycled and development in science and technology are maked rapid progress, it is little that we are seeking a kind of investment always, simple to operate, operation and maintenance cost is low, the practical CO purification technique that product purity is high, polymeric membrane has produced keen interest in recent years growth momentum and at the achievement let us of obtaining aspect the gas separation to the technology of taking embrane method to reclaim acetate acid tail gas, by a series of technological demonstration and material type selecting determined general in gloomy membrane separation and purification technology.
But membrane separation technique is produced in the high pressure exhaust gas recovery of acetate at carbonylation at present to advancing having relatively high expectations of film gas, owing to exist acetic acid, moisture etc. to be easy to the hurtful component of film in the tail gas, can't directly use membrane separation technique.
Summary of the invention
The high pressure exhaust gas of producing acetate for the carbonylation that solves the prior art existence can't directly use membrane separation technique, the invention provides a kind of embrane method and reclaim the method that carbonylation is produced CO in the acetate high pressure exhaust gas, adopt membrane separating method recovery CO wherein, CO content 〉=91% (molar content) in the product gas by tail gas after the preliminary treatment.
Technical scheme of the present invention is: a kind of embrane method reclaims the method that carbonylation is produced CO in the acetate high pressure exhaust gas, and tail gas compresses three steps through preliminary treatment, film separation, gas:
Preliminary treatment: temperature is that 40～60 ℃, pressure are that 2.6～2.8MPa, flow are 2000m
3/ h-6000m
3The acetic acid high pressure mixing tail gas of/h enters aeration tower, contacts with demineralized water from top to bottom is reverse at Ta Nei, and acetic acid content≤100ppm in the aeration tower outlet acetate acid tail gas, the demineralized water internal circulating load of aeration tower is 0.5～1.0m
3/ h.Enter demister by the aeration tower tail gas discharged and further remove wherein droplets entrained, control demister liquid level 150～200mm; Enter association filter by the demister tail gas discharged, 0.01 micron of filtering accuracy; The tail gas discharged heater via is heated to 40～60 ℃;
Film separates: through pretreated tail gas enter general in gloomy membrane separator, the rate of rise≤0.3MPa/min;
The gas compression: the tail gas that separates through film enters compressor, and flow is 1000m
3/ h-3000m
3/ h, product gas is recycled again, reduce internal heat torch burning of hydrogen rich gas.
Described embrane method reclaims carbonylation and produces the device that the method for CO in the acetate high pressure exhaust gas is used, mainly by aeration tower, demister, association filter, heater, general in gloomy membrane separator, compressor form, aeration tower links to each other with demister by pipeline, demister links to each other with association filter by pipeline, association filter links to each other with heater by pipeline, heater by pipeline with general in gloomy separator be connected, general in gloomy separator be connected with compressor by pipeline.Described general in gloomy film be two groups of totally 32 membrane modules, be the polyimides hollow-fibre membrane.
Beneficial effect: 1. produce in the acetate high pressure exhaust gas for carbonylation and cause the component methyl iodide, acetic acid, moisture etc. of damage to remove by aeration tower to film, the absorption tower of the acetic acid high pressure exhaust gas access to plant pretreatment system of regime flow, carry out reverse the contact at Ta Nei with from top to bottom demineralized water, in the tower is tower plate structure, by controlling the water internal circulating load harmful components such as the acetic acid in the tail gas, moisture are removed, make acetic acid content≤100ppm in the tail gas;
2. remove droplets entrained in the tail gas by demister, to prevent impact effect when film separates, the infringement membrane module;
3. remove contaminant particles in the tail gas by association filter and reduce infringement membrane module;
4. acetic acid high pressure mixing tail gas is that 2.6～2.8MPa, flow are 2000m at pressure
3/ h-6000m
3The amount of/h, and the last flow that reclaims product gas of control is 1000m
3/ h-3000m
3/ h avoids N
2The accumulation influence that operation steady in a long-term produces to the film system;
5. pass through steam heater in this method, the mixed tail gas temperature is raise, make it enter the film system and separate away from the moisture dew point.Mixed tail gas enters behind the membrane separator shell along the fiber flows outside, the low-pressure side enrichment and go out the film separation system torch that reduces internal heat as the infiltration conductance and burn CO, N that infiltration rate is slower in pipe of hydrogen selective ground penetrated preferably fiber membranous wall
2Then be trapped in non-infiltrating gas side, pressure and unstripped gas are approaching, and guiding system forms product gas and enters compression stage.The present invention controls the rate of recovery by the flow of adjusting unstripped gas, hydrogen rich gas, product gas, by gas compressor the product gas lift is depressed into the system pressure balance and incorporates system into, the content of CO in the final products gas 〉=91% molar content.
6. the present invention proposes utilize general in gloomy film recycle the method for acetic acid high pressure exhaust gas, the pressure swing adsorption method isolation technics of comparing does not have that phase transformation, energy consumption are low, unit scale requires changeablely according to what handle tolerance, and equipment is simple, easy to operate, operational reliability is high.Since device comes into operation, both reach the purpose of continuous recovery CO, reached the needs of environmental protection again.
Description of drawings
Fig. 1 is an acetic acid high pressure exhaust gas process chart, and aeration tower, demister, association filter, heater have constituted the gas pretreatment system that advances before the film.
T1 is an aeration tower, and X1 is a demister, and X1B is an association filter, and E1 is a heater, and M1 is a membrane separator, and C1 is a compressor.
Fig. 2 is an acetic acid high pressure exhaust gas recovery process sketch.
The specific embodiment
Now whole separation process is explained in conjunction with Fig. 1, Fig. 2:
1. aeration tower T1:
1) acetic acid mixed high-voltage exhaust flow is 2000m
3/ h-6000m
3/ h, the aeration tower operating pressure is 2.6～2.8MPa, temperature is 40～60 ℃, in be two Floor 12 stainless steel valve platies, the acetic acid high pressure exhaust gas behind aeration tower in the absorption liquid acetic acid mass content be 30%;
2) the aeration tower circulating pump is delivered to cat head with demineralized water, and demineralized water contacts with the acetic acid high pressure exhaust gas is reverse, and the demineralized water internal circulating load is 0.5～1.0m
3/ h looks acetic acid content in the tail gas is adjusted internal circulating load, makes acetic acid content≤100ppm in the aeration tower outlet acetic acid high pressure exhaust gas;
3) discharge on the stable control aeration tower, liquid level at the bottom of the stabilizer, waste acid liquor is recycled;
2. demister X1: the droplet of carrying secretly in the acetic acid high pressure exhaust gas is effectively removed control demister liquid level 150～200mm, discharge opeing regularly.Liquid level is provided with interlocking protective device, prevents that entrained liquid from seriously having a negative impact to membrane lifetime.
3. association filter X1B: the particle particulate that carries in the acetic acid high pressure exhaust gas is removed, prevent to stop up general in gloomy film to the influence of membrane separating effect, 0.01 micron of filtering accuracy guarantees the filter working stability by the monitoring to pressure reduction.
4. heater E1: the acetic acid high pressure exhaust gas is not a saturated gas after above-mentioned processing, and moisture can have influence on the use of film, by public work 0.6MPa low-pressure steam tail gas is heated to 40～60 ℃, makes tail gas away from dew point.Realize temperature controlling, indication, warning and interlocking by steam flow control valve, temperature transmitter, with the constant gas temperature.Condensed water in the whole device removes trench.
5. gloomy membrane separator M1 in general
1) device uses diffusion barrier as U.S. product general in gloomy doughnut, material is a polyimides, 2 groups of totally 32 membrane modules;
2) the gloomy separator rate of rise≤0.3MPa/min in general need open the raw material gas inlet main valve of every group of membrane separator that will come into operation, the outlet main valve of products C O gas, the outlet valve of hydrogen rich gas side when the pressure of gloomy membrane separator rises to preceding system pressure balance in general;
3) by control valve control and regulation product atmospheric pressure, flow and CO content, guarantee that the tail-gas compressor inlet pressure is stable.
6. compressor C1
The product throughput is that flow is 1000m
3/ h-3000m
3/ h, tail-gas compressor incorporate the utilization of acetic acid system recoveries into after film product gas being reached the working pressure of next step after by 2.1～2.3MPa boost in pressure;
The control of acetate acid tail gas yield, the rate of recovery in this method
1) yield: Membrane recovery unit MRU can be realized recovery and the utilization of CO, but nitrogen can not effectively be separated, and therefore can cause the accumulation of nitrogen in the system, among the present invention by realizing the reduce internal heat continuous recovery of adjustment realization tail gas of torch emptying amount and yield of tail gas.By the calculating of nitrogen material balance among acetic acid house steward CO in the present device, the implement device high pressure exhaust gas reclaims the adjustment balance of tolerance, and nitrogen recycling amount and hydrogen rich gas emptying amount are consistent.
2) rate of recovery: the gloomy film system in general of guaranteeing can realize the CO in the long-term recovery acetic acid high pressure exhaust gas of maximum, guarantee CO content 〉=91%, by adjusting film tolerance, product tolerance, in guaranteeing the acetic acid house steward, recycle the acetic acid high pressure exhaust gas during CO proportion to greatest extent.
Embodiment 1
By above embodiment as can be seen, this cover membrane separation device can reach purpose of design after actual putting into operation, and product gas CO content reaches more than 91%, satisfies technological requirement, has realized the continuous recycling of acetic acid high pressure exhaust gas.
By the pretreatment system that aeration tower, demister, association filter are formed, " being harmful to " component in the tail gas is removed, prevent from the stable operation of film is exerted an influence; Select for use in actual applications 2 groups general in gloomy film realized effective separation to tail gas, handle tolerance, product pneumatolytic and divide and all reached job requirement, realized optimum organization; By example as can be seen film to N
2Can not effectively remove, so the present invention in time adjusts the tolerance that product gas advances acetic acid by the calculating of material balance and prevents N
2Accumulation.
Claims (4)
1. an embrane method reclaims the method that carbonylation is produced CO in the acetate high pressure exhaust gas, it is characterized in that, tail gas compresses three steps through preliminary treatment, film separation, gas:
Preliminary treatment: temperature is that 40～60 ℃, pressure are that 2.6～2.8MPa, flow are 2000m
3/ h-6000m
3The acetic acid high pressure mixing tail gas of/h enters aeration tower, contacts acetic acid content≤100ppm in the aeration tower outlet acetate acid tail gas with demineralized water from top to bottom is reverse at Ta Nei; Enter demister by the aeration tower tail gas discharged and further remove wherein droplets entrained, control demister liquid level 150～200mm, liquid level is provided with interlocking protective device; Enter association filter by the demister tail gas discharged, 0.01 micron of filtering accuracy; The tail gas discharged heater via is heated to 40～60 ℃;
Film separates: through pretreated tail gas enter general in gloomy membrane separator, the rate of rise≤0.3MPa/min;
The gas compression: the tail gas that separates through film enters compressor, and flow is 1000m
3/ h-3000m
3/ h, product gas is recycled again, reduce internal heat torch burning of hydrogen rich gas.
2. embrane method as claimed in claim 1 reclaims the method that carbonylation is produced CO in the acetate high pressure exhaust gas, it is characterized in that the demineralized water internal circulating load of aeration tower is 0.5～1.0m
3/ h.
3. embrane method as claimed in claim 1 reclaims carbonylation and produces the device that the method for CO in the acetate high pressure exhaust gas is used, it is characterized in that, mainly by aeration tower, demister, association filter, heater, general in gloomy membrane separator, compressor form, aeration tower links to each other with demister by pipeline, demister links to each other with association filter by pipeline, association filter links to each other with heater by pipeline, heater by pipeline with general in gloomy separator be connected, general in gloomy separator be connected with compressor by pipeline.
4. embrane method as claimed in claim 3 reclaims carbonylation and produces the device that the method for CO in the acetate high pressure exhaust gas is used, and it is characterized in that, described general in gloomy film be two groups of totally 32 membrane modules, be the polyimides hollow-fibre membrane.
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|---|---|---|---|
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|---|---|---|---|
| CN200810235144XA CN101439256B (en) | 2008-11-14 | 2008-11-14 | Film method for recycling CO in high-pressure exhaust from production of acetic acid by carbonylation |
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| CN101439256B true CN101439256B (en) | 2011-01-12 |
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| US5840969A (en) * | 1996-11-29 | 1998-11-24 | Haldor Topsoe A/S | Process for the preparation of acetic acid from a synthesis gas of hydrogen and carbon monoxide |
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| CN1520920A (en) * | 2003-01-30 | 2004-08-18 | 西南化工研究设计院 | Technique for recovering useful constituent from the tail gas arising from acetic acid synthesis process from carbonyl |
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| US9353034B2 (en) | 2012-02-07 | 2016-05-31 | Celanese International Corporation | Hydrogenation process with reduced residence time for vapor phase reactants |
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